Classifications

• • C—CHEMISTRY; METALLURGY
  • C01—INORGANIC CHEMISTRY
  • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
  • C01B33/00—Silicon; Compounds thereof
  • C01B33/113—Silicon oxides; Hydrates thereof
  • C01B33/12—Silica; Hydrates thereof, e.g. lepidoic silicic acid
  • C01B33/126—Preparation of silica of undetermined type
  • C01B33/128—Preparation of silica of undetermined type by acidic treatment of aqueous silicate solutions
• • C—CHEMISTRY; METALLURGY
  • C01—INORGANIC CHEMISTRY
  • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
  • C01B33/00—Silicon; Compounds thereof
  • C01B33/113—Silicon oxides; Hydrates thereof
  • C01B33/12—Silica; Hydrates thereof, e.g. lepidoic silicic acid
  • C01B33/18—Preparation of finely divided silica neither in sol nor in gel form; After-treatment thereof
  • C01B33/187—Preparation of finely divided silica neither in sol nor in gel form; After-treatment thereof by acidic treatment of silicates
  • C01B33/193—Preparation of finely divided silica neither in sol nor in gel form; After-treatment thereof by acidic treatment of silicates of aqueous solutions of silicates

Definitions

• the present invention relates to a new process for the preparation of precipitated silica.
• precipitated silicas as a catalyst support, as an absorbent of active materials (in particular liquid carriers, for example used in foodstuffs, such as vitamins (especially vitamin E, choline chloride), as a viscosifying, texturizing or anti-caking agent, as an element for battery separators, as an additive for toothpaste, for paper.
• active materials in particular liquid carriers, for example used in foodstuffs, such as vitamins (especially vitamin E, choline chloride), as a viscosifying, texturizing or anti-caking agent, as an element for battery separators, as an additive for toothpaste, for paper.
• precipitated silicas as reinforcing filler in silicone matrices (for example for coating electrical cables) or in compositions based on polymer (s), natural or synthetic, in particular elastomer (s), especially diene, for example for shoe soles, floor coverings, gas barriers, fire-retardant materials and also technical parts such as ropeway rollers, appliance seals, liquid or gas line joints, brake system seals, ducts, cables and transmission belts.
• the object of the present invention is to provide a new process for the preparation of precipitated silica, which constitutes an alternative to the known processes for the preparation of precipitated silica.
• one of the aims of the present invention is to provide a process which, while having an improved productivity in particular at the level of the precipitation reaction, in particular with respect to the preparation methods of the state of the art involving using a dilute acid as acid, it is possible to obtain precipitated silicas having physicochemical characteristics and similar properties, in particular as regards their morphology, particle size and porosity and / or their reinforcing properties, to those of precipitated silicas obtained by these preparative methods of the state of the art.
• Another object of the invention is preferably, at the same time, to reduce the amount of energy consumed and / or the amount of water used in the preparation of precipitated silica, particularly with respect to the methods of the state of the art. the technique employing as acid a dilute acid.
• the object of the invention is a new process for the preparation of precipitated silica, comprising the reaction of a silicate with at least one acid, whereby a suspension of silica is obtained, followed by separation and drying of this suspension, in which the reaction of the silicate with the acid is carried out according to the following successive steps:
• silicate and acid are added simultaneously to the reaction medium, so that the pH of the reaction medium is maintained between 7 and 10, preferably between 7.5 and 9.5,
• step (vi) the reaction medium obtained at the end of step (v) is brought into contact (mixture) (thus having a pH of between 2.5 and 5.3, preferably between 2.8 and 5.2 ) with acid and silicate, such that the pH of the reaction medium is maintained between 2.5 and 5.3, preferably between 2.8 and 5.2, in which process: in at least a part of step (ii) (i.e. in at least some or all of step (ii))
• the acid used is a concentrated acid, preferably selected from the group consisting of sulfuric acid having a concentration of at least 80% by weight, in particular at least 90% by weight, acetic acid or formic acid having a concentration of at least 90% by weight, the nitric acid having a concentration of at least 60% by weight, the phosphoric acid having a concentration of at least 75% by weight, the acid hydrochloric acid having a concentration of at least 30% by mass.
• the concentrated acid is concentrated sulfuric acid, that is to say sulfuric acid having a concentration of at least 80% by weight, preferably at least 90% by weight. .
• sulfuric acid having a concentration of at least 1400 g / l, in particular at least 1650 g / l.
• step (vii) it is possible, in a subsequent step (vii), to add, in the reaction medium obtained at the end of step (vi), an alkaline agent, preferably a silicate, until it reaches pH value of the reaction medium of between 4.7 and 6.3, preferably between 5.0 and 5.8, for example between 5.0 and 5.4.
• an alkaline agent preferably a silicate
• the acid used in step (vi) is a concentrated acid as defined above.
• the acid used in steps (ii), (iv) and (v) can then be a dilute acid, advantageously dilute sulfuric acid, that is to say having a concentration much lower than 80% in bulk, in this case a concentration of less than 20% by weight (and in general of at least 4% by weight), in particular less than 14% by weight, in particular of not more than 10% by weight, for example between 5 and 10% by weight.
• a dilute acid advantageously dilute sulfuric acid, that is to say having a concentration much lower than 80% in bulk, in this case a concentration of less than 20% by weight (and in general of at least 4% by weight), in particular less than 14% by weight, in particular of not more than 10% by weight, for example between 5 and 10% by weight.
• the invention is a new process for the preparation of precipitated silica comprising the reaction of a silicate with at least one acid, whereby a suspension of silica is obtained. , then separating and drying this suspension, in which the reaction of the silicate with the acid is carried out according to the following successive steps: (i) forming an aqueous base having a pH of between 2 and 5, preferably between 2.5 and 5, (ii) adding to said base of the tank, simultaneously, silicate and acid, of in such a way that the pH of the reaction medium is maintained between 2 and 5, preferably between 2.5 and 5,
• silicate and acid are added simultaneously to the reaction medium, so that the pH of the reaction medium is maintained between 7 and 10, preferably between 7.5 and 9.5,
• step (vi) the reaction medium obtained at the end of step (v) is brought into contact (mixture) (thus having a pH of between 2.5 and 5.3, preferably between 2.8 and 5.2 ) with acid and silicate, so that the pH of the reaction medium is maintained between 2.5 and 5.3, preferably between 2.8 and 5.2, in which process, in at least a part of step (ii) (i.e., in at least a part or all of step (ii)), the acid used is a concentrated acid, preferably selected from the group formed with sulfuric acid having a concentration of at least 80% by weight, in particular at least 90% by weight, the acetic acid or the formic acid having a concentration of at least 90% by weight, nitric acid having a concentration of at least 60% by weight, the phosphoric acid having a concentration of at least 75% by weight, the hydrochloric acid having a concentration of at least 30% by weight.
• mixture thus having a pH of between 2.5 and 5.3, preferably between 2.8 and 5.2
• step (ii) is a concentrated acid, preferably selected from the group consisting of sulfuric acid having a concentration of at least 80% by weight, in particular at least 90% by weight.
• acetic acid or formic acid having a concentration of at least 90% by weight
• the nitric acid having a concentration of at least 60% by weight
• the phosphoric acid having a concentration of at least 75% by weight
• the hydrochloric acid having a concentration of at least 30% by weight.
• the concentrated acid is concentrated sulfuric acid, that is to say sulfuric acid having a concentration of at least 80% by weight (and generally at most 98% by weight). mass), preferably at least 90% by weight; in particular, its concentration is between 90 and 98% by weight, for example between 91 and 97% by weight.
• the concentrated acid as defined above is used only in part of step (ii).
• the acid used in steps (iv) to (vi) can then be, for example, a dilute acid, advantageously dilute sulfuric acid, that is to say having a concentration of much less than 80% by weight. , in this case a concentration of less than 20% by weight (and in general of at least 4% by weight), in particular less than 14% by weight, in particular of not more than 10% by weight, for example between 5 and 10% by weight.
• a dilute acid advantageously dilute sulfuric acid, that is to say having a concentration of much less than 80% by weight.
• a concentration of less than 20% by weight (and in general of at least 4% by weight) in particular less than 14% by weight, in particular of not more than 10% by weight, for example between 5 and 10% by weight.
• the acid used in step (iv) is also a concentrated acid as mentioned above.
• the acid used in steps (iv) and (v) is also a concentrated acid as mentioned above.
• the acid used in steps (iv) to (vi) is also a concentrated acid as mentioned above.
• the concentrated acid used in a part of step (ii) is generally used in a second and last part of this step (ii) (the acid used in the other part of step (ii) being for example a diluted acid as described above).
• the acid employed until the gel point is reached in the reaction medium may be a dilute acid as mentioned above, advantageously dilute sulfuric acid (this is that is, a concentration of less than 80% by weight, in this case a concentration of less than 20% by weight, generally less than 14% by weight, in particular of not more than 10% by weight, for example between 5 and 10% by weight).
• the acid employed after reaching the gel point in the reaction medium can itself be a concentrated acid as mentioned above, advantageously concentrated sulfuric acid, that is to say acid sulfuric acid having a concentration of at least 80% by weight, preferably at least 90% by weight, in particular between 90 and 98% by weight.
• the acid employed in the first x minutes of step (ii), with x being between 10 and 25, preferably between 12 and 22, may be a dilute acid as mentioned above and the acid employed after the first x minutes of step (ii), with x between 10 and 25, preferably between 12 and 22, may be a concentrated acid as mentioned above.
• the acid used in the whole of step (ii) may also be a concentrated acid as mentioned above, advantageously acid concentrated sulfuric acid, that is to say having a concentration of at least 80% by weight, preferably at least 90% by weight, in particular between 90 and 98% by weight.
• water may optionally be added to the initial stock, in particular either before step (ii) or during step (ii).
• acid (s) (concentrated acid or dilute acid) an organic acid such as acetic acid, formic acid or carbonic acid or, preferably, a mineral acid such as sulfuric acid, nitric acid, phosphoric acid or hydrochloric acid.
• organic acid such as acetic acid, formic acid or carbonic acid or, preferably, a mineral acid such as sulfuric acid, nitric acid, phosphoric acid or hydrochloric acid.
• concentrated acetic acid or concentrated formic acid is used as the concentrated acid, then their concentration is at least 90% by weight.
• concentrated nitric acid is used as concentrated acid, then its concentration is at least 60% by weight.
• concentrated concentrated phosphoric acid If concentrated concentrated phosphoric acid is used, then its concentration is at least 75% by weight. If concentrated hydrochloric acid is used as concentrated acid, then its concentration is at least 30% by weight.
• the acid (s) used is sulfuric acid (s), the concentrated sulfuric acid then used having a concentration as already mentioned in the above discussion.
• silicate any current form of silicates such as metasilicates, disilicates and advantageously an alkali metal silicate, in particular sodium or potassium silicate.
• the silicate may have a concentration (expressed as SiO 2) of between 40 and 330 g / l, for example between 60 and 300 g / l, in particular between 60 and 260 g / l.
• the silicate used is sodium silicate.
• sodium silicate In the case where sodium silicate is used, it generally has a weight ratio SiO 2 / Na 2 O of between 2.5 and 4, for example between 3.2 and 3.8.
• the alkaline agent employed in the optional step (vii) may be, for example, a solution of sodium hydroxide, potassium hydroxide or ammonia.
• this alkaline agent is silicate, in particular silicate as used in the preceding steps.
• reaction of the silicate with the acid is in a very specific manner according to the following steps.
• First (step (i)) is formed an aqueous base stock having a pH of between 2 and 5.
• the heelstock formed has a pH of between 2.5 and 5, in particular between 3 and 4.6; this pH is for example between 3.5 and 4.5.
• This initial starter can be obtained (preferred variant) by adding acid to water so as to obtain a pH value of the bottom of the tank between 2 and 5, preferably between 2.5 and 5, especially between 3 and 4.6 and for example between 3.5 and 4.5.
• It can also be obtained by adding acid to a water + silicate mixture so as to obtain this pH value. It can also be prepared by adding acid to a stock base containing silica particles previously formed at a pH below 7, so as to obtain a pH value between 2 and 5, preferably between 2.5 and 5. , especially between 3 and 4.6 and for example between 3.5 and 4.5.
• the heelstock formed in step (i) may or may not comprise an electrolyte.
• electrolyte is here understood in its normal acceptation, that is to say that it signifies any ionic or molecular substance which, when in solution, decomposes or dissociates to form ions or charged particles.
• electrolyte mention may be made of a salt of the group of alkali and alkaline earth metal salts, in particular the salt of the starting silicate metal and of the acid, for example sodium chloride in the case of the reaction of a silicate of sodium with hydrochloric acid or, preferably, sodium sulfate in the case of the reaction of a sodium silicate with sulfuric acid.
• sodium sulfate when sodium sulfate is used as the electrolyte in step (i), its concentration in the initial stock is in particular between 12 and 20 g / l, for example between 13 and 18 g. / L.
• the second step (step (ii)) consists of a simultaneous addition of acid and of silicate, in such a way (particularly at such flow rates) that the pH of the reaction medium is between 2 and 5, preferably between 2, 5 and 5, especially between 3 and 5, for example between 3.5 and 4.8.
• this simultaneous addition is carried out in such a way that the pH value of the reaction medium is close, preferably constant (within ⁇ 0.2), to that reached at the end of the initial step (i). .
• a step (iii) the addition of acid is stopped while continuing the addition of silicate in the reaction medium so as to obtain a pH value of the reaction medium of between 7 and 10, preferably between 7 and 10. , 5 and 9.5, for example between 7.5 and 9.
• step (iii) it is possible to carry out, just after this step (iii) and therefore just after stopping the addition of silicate, a ripening of the reaction medium, in particular at the pH obtained at the end of step (iii), and in general with stirring; this curing can for example last from 2 to 45 minutes, in particular from 5 to 25 minutes, and preferably does not include any addition of acid or addition of silicate.
• a new simultaneous addition of acid and silicate in such a way (particularly at such flow rates) that the pH of the reaction medium is maintained between 7 and 10 preferably between 7.5 and 9.5, for example between 7.5 and 9 (step (iv)).
• this second simultaneous addition is carried out in such a way that the pH value of the reaction medium is constantly equal (within ⁇ 0.2) to that reached at the end of the previous step.
• step (iii) and step (iv) for example between, on the one hand, the eventual maturing according to step (iii), and, of on the other hand, step (iv), add to the reaction medium acid, preferably concentrated acid as defined above, the pH of the reaction medium after the addition of acid being, however, between 7 and 9.5, preferably between 7.5 and 9.5, for example between 7.5 and 9. Then, in a step (v), the silicate addition is stopped while continuing the addition of acid in the reaction medium so as to obtain a pH value of the reaction medium of between 2.5 and 5.3, preferably between 2.8 and 5.2, for example between 3.5 and 5.1 ( even between 3.5 and 5.0).
• step (v) a ripening of the reaction medium, in particular at the pH obtained after step (v), and in general with stirring; this curing can for example last from 2 to 45 minutes, in particular from 5 to 20 minutes, and preferably does not comprise any addition of acidifying agent or addition of silicate.
• reaction medium obtained at the end of stage (v) said reaction medium having a pH of between 2.5 and 5.3, preferably between 2.8 and 5.2, for example between 3.5 and 5.1 (or even 3.5 to 5.0),
• the pH of the reaction medium obtained is maintained between 2.5 and 5.3, preferably between 2.8 and 5.2, for example between 3.5 and 5.1. (even between 3.5 and 5.0).
• Said pH of the reaction medium may vary within the range 2.5-5.3, preferably in the range 2.8-5.2, for example in the range 3.5-5.1 (even 3 , 5-5,0), or, preferably, remain (substantially) constant within these ranges.
• the contacting of the reaction medium resulting from step (v) with the acid and the silicate is carried out by adding acid and silicate to said reaction medium.
• step (vi) the acid and then the silicate are added to said reaction medium.
• step (vi) the acid and the silicate are added simultaneously to said reaction medium; preferably, this simultaneous addition is carried out with regulation of the pH of the reaction medium obtained during this addition to a value (substantially) constant within the aforementioned ranges.
• Step (vi) is generally carried out with stirring.
• step (vii) of the process according to the invention consists in an addition, in the reaction medium obtained at the end of step (vi), of an alkaline agent, preferably of silicate, and this up to to reach a pH value of the reaction medium of between 4.7 and 6.3, preferably between 5.0 and 5.8, for example between 5.0 and 5.4.
• an alkaline agent preferably of silicate
• This step (vii) is usually carried out with stirring.
• the whole reaction steps (i) to (vi), or (vii) where appropriate) is carried out with stirring.
• all the steps are carried out at a constant temperature.
• the end-of-reaction temperature is higher than the reaction start temperature: thus, the temperature is maintained at the beginning of the reaction (for example during steps (i) and (ii)) preferably between 75 and 90 ° C, then the temperature is increased, preferably to a value between 90 and 97 ° C, the value at which it is maintained (for example during steps (iii) to (vii)) until the end of the reaction. It may be advantageous to proceed at the end of step (vi), or of optional step (vii), to a maturation of the reaction medium obtained, in particular at the pH obtained at the end of this step (vi) (or step (vii)), and in general with stirring.
• This ripening can for example last from 2 to 30 minutes, in particular 3 to 20 minutes and can be carried out between 75 and 97 ° C, preferably between 80 and 96 ° C, in particular at the temperature at which step (vii) (or step (vii)). It preferably does not include any addition of acid or addition of silicate.
• step (vi) may be carried out in a fast mixer or in a turbulent flow zone, which may allow better control of the characteristics of the precipitated silicas obtained.
• silicate with the medium resulting from the addition of the acid to the reaction medium obtained at the end of step (v) can be carried out in a fast mixer or in a turbulent flow zone.
• step (vi) the acid and the silicate are added simultaneously to the reaction medium obtained at the end of step (v), then bringing said acid into contact with said silicate with said reaction medium can be carried out in a fast mixer or in a turbulent flow zone.
• the reaction medium obtained in the fast mixer or in a turbulent flow zone feeds a reactor, preferably subjected to agitation, reactor in which the possible step (vii) is implemented.
• step (vi) it is possible to use a fast mixer chosen from symmetrical T-mixers or Y-mixers, asymmetric T-shaped or Y-shaped mixers (or tubes), tangential jet mixers, mixers Hartridge-Roughton, vortex mixers, rotor-stator mixers.
• a fast mixer chosen from symmetrical T-mixers or Y-mixers, asymmetric T-shaped or Y-shaped mixers (or tubes), tangential jet mixers, mixers Hartridge-Roughton, vortex mixers, rotor-stator mixers.
• T or symmetrical Y are usually made of two opposite tubes (T-tubes) or forming an angle less than 180 ° (Y-tubes), of the same diameter, discharging into a central tube whose diameter is identical to or greater than that of the two previous tubes. They are called "symmetrical" because the two reagent injection tubes have the same diameter and the same angle with respect to the central tube, the device being characterized by an axis of symmetry.
• the central tube has a diameter about twice as large as the diameter of the opposed tubes; similarly the fluid velocity in the central tube is preferably half that in the opposite tubes.
• a mixer or tube T or Y asymmetrical rather than a symmetrical T or Y mixer.
• one of the fluids (the lower flow fluid in general) is injected into the central tube by means of a smaller diameter side tube.
• the latter forms with the central tube an angle of 90 ° in general (T-tube); this angle may be different from 90 ° (Y-tube), giving co-current systems (for example 45 ° angle) or counter-current (for example 135 ° angle) relative to the other current.
• a fast mixer As a fast mixer, a tangential jet mixer, a Hartridge-Roughton mixer or a vortex mixer (or precipitator) are preferably used, which are derived from symmetrical T-shaped devices.
• step (vi) it is possible to use a tangential jet mixer, Hartridge-Roughton or vortex, comprising a chamber having (a) at least two tangential admissions through which enter separately (but at the same time ) on the one hand, the silicate, and, on the other hand, the medium resulting from the addition of acid to the reaction medium resulting from stage (v), ie, on the one hand, silicate and the acid, and, on the other hand, the reaction medium resulting from step (v), and (b) an axial outlet through which the reaction medium obtained in this step (vi) leaves, preferably to a reactor (tank) arranged in series after said mixer.
• the two tangential admissions are preferably located symmetrically, and oppositely, with respect to the central axis of said chamber.
• the mixer chamber with tangential jets, Hartridge-Roughton or vortex optionally used generally has a circular section and is preferably of cylindrical shape.
• Each tangential inlet tube may have an internal diameter d of 0.5 to 80 mm.
• This internal diameter d may be between 0.5 and 10 mm, in particular between 1 and 9 mm, for example between 2 and 7 mm. However, especially on an industrial scale, it is preferably between 10 and 80 mm, in particular between 20 and 60 mm, for example between 30 and 50 mm.
• the internal diameter of the chamber of the tangential jet mixer, Hartridge-Roughton or vortex optionally used may be between 3d and 6d, in particular between 3d and 5d, for example equal to 4d; the internal diameter of the axial outlet tube may be between 1 d and 3d, in particular between 1.5d and 2.5d, for example equal to 2d.
• step (vi) or of step (vii) if appropriate, a silica slurry is obtained, which may be followed by maturing. separated (liquid-solid separation).
• the separation used in the preparation process according to the invention usually comprises a filtration, followed by washing if necessary.
• the filtration is carried out by any suitable method, for example by means of a filter press, a belt filter, a vacuum filter.
• the silica suspension thus recovered (filter cake) is then dried.
• This drying can be done by any means known per se.
• the drying is done by atomization.
• any suitable type of atomizer may be used, such as a turbine, nozzle, liquid pressure or two-fluid atomizer.
• a turbine nozzle
• liquid pressure two-fluid atomizer.
• the filter cake is not always under conditions allowing atomization, in particular because of its high viscosity.
• the cake is then subjected to a disintegration operation. This operation can be performed mechanically, by passing the cake in a colloid mill or ball.
• the disintegration is generally carried out in the presence of water and / or in the presence of an aluminum compound, in particular sodium aluminate and, optionally, in the presence of an acid as described above (in the latter case the aluminum compound and the acid are usually added simultaneously).
• the disintegration operation makes it possible in particular to lower the viscosity of the suspension to be dried later.
• the silica that can then be obtained is usually in the form of substantially spherical balls.
• the silica that is then likely to be obtained is generally in the form of a powder.
• the silica that may then be obtained may be in the form of a powder.
• the dried product in particular by a turbine atomizer or milled as indicated above can optionally be subjected to a step agglomerating, which consists for example of a direct compression, a wet-path granulation (that is to say with use of a binder such as water, suspension of silica, etc.), an extrusion or, preferably, dry compaction.
• a step agglomerating which consists for example of a direct compression, a wet-path granulation (that is to say with use of a binder such as water, suspension of silica, etc.), an extrusion or, preferably, dry compaction.
• the silica that can then be obtained by this agglomeration step is generally in the form of granules.
• the powders, as well as the silica beads, obtained by the process according to the invention thus offer the advantage, among others, of having a simple, effective and economical way of accessing granules, in particular by conventional setting operations. in form, such as for example a granulation or compaction, without the latter causing degradation likely to hide or annihilate the good intrinsic properties attached to these powders or beads.
• the process according to the invention makes it possible to obtain silicas formed from aggregates of large primary silica particles on the surface of which there are small primary silica particles advantageously having the characteristics of the silicas described in the international application WO 201 1/026895.
• the implementation of the preparation method according to the invention makes it possible in particular to obtain during said process (at the end of step (vi) or of the possible step (vii)) a suspension more concentrated in silica than that obtained by an identical process using only dilute acid, and therefore a gain in productivity of silica (can reach for example at least 10 to 40%) , while surprisingly accompanying the production of precipitated silicas preferably having a particular morphology, particle size and porosity.
• the precipitated silicas obtained by the process according to the invention have a good dispersibility in the polymers and give them a compromise of very satisfactory properties, for example with regard to their comparable mechanical, dynamic and rheological properties.
• the process according to the invention makes it possible, compared with an identical process using only dilute acid, to gain energy consumption (in the form of live steam, for example), in particular to the precipitation reaction (that is to say at the end of the step (vi)), due to a decrease in the quantities of water involved and the exo-thermicity associated with the use of concentrated acid.
• the use of concentrated acid makes it possible to restrict (for example by at least 15%) the quantity of water required for the reaction, in particular because of the reduction in the quantity of water used for the preparation of acid.
• the precipitated silicas prepared by the process according to the invention can be used in many applications.
• They can be used in particular as a catalyst support, as absorbent of active substances (in particular liquid carriers, for example used in foodstuffs, such as vitamins (vitamin E), choline chloride), in polymer compositions. (S), including elastomer (s), silicone (s), as viscosifying agent, texturizing or anti-caking agent, as an element for battery separators, as an additive for toothpaste, for concrete, for paper.
• active substances in particular liquid carriers, for example used in foodstuffs, such as vitamins (vitamin E), choline chloride
• S including elastomer (s), silicone (s), as viscosifying agent, texturizing or anti-caking agent, as an element for battery separators, as an additive for toothpaste, for concrete, for paper.
• the polymer compositions in which they may be used, especially as reinforcing filler, are generally based on one or more polymers or copolymers, in particular one or more elastomers, in particular thermoplastic elastomers, having preferably, at least a glass transition temperature of between -150 and +300 ° C, for example between -150 and +20 ° C.
• diene polymers in particular diene elastomers.
• finished articles based on the polymer compositions described above, such as shoe soles, tires, floor coverings, gas barriers, fireproofing materials and the like. also technical parts such as ropeway rollers, appliance gaskets, liquid or gas line joints, braking system seals, ducts (especially cable ducts), cables and belts transmissions.

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